MX2014002923A

MX2014002923A - Novel catalyst to increase propylene yields from a fluid catalytic cracking unit.

Info

Publication number: MX2014002923A
Application number: MX2014002923A
Authority: MX
Inventors: David H Harris
Original assignee: Basf Corp
Priority date: 2011-09-13
Filing date: 2012-09-13
Publication date: 2014-10-01
Also published as: MX342783B; EP2755763A1; CN107670688A; BR112014005898A2; JP6133989B2; JP2015533639A; EP2755763A4; CN103945940A; US20130066131A1; KR20140090597A; US9227181B2; CA2845414A1

Abstract

A catalyst composition resulting in increased propylene yields during fluid catalytic cracking processes comprises (i) Y zeolite, (ii) ZSM-5 zeolite, and (iii) Beta zeolite.

Description

NEW CATALYST TO INCREASE PROPYLENE PERFORMANCE TO STARTING FROM A FLUID CATALYTIC CRAQUEO UNIT Field of the invention The present invention provides a novel catalyst composition for increasing the yields of propylene during fluid catalytic cracking.

BACKGROUND OF THE INVENTION Catalytic cracking, and particularly fluid catalytic cracking (FCC), is routinely used to convert heavy hydrocarbon feedstocks into lighter products, such as gasoline and fractions in the range of distillates. However, there is a growing need to enhance the yield of light olefins, especially propylene, in the product range from catalytic cracking processes. Light olefins (C2-C4 olefins) are important raw materials for the petrochemical industry. Propylene, for example, a light olefin hydrocarbon with three carbon atoms per molecule, is an important chemical for use in the production of other useful materials, such as polypropylene. Polypropylene is one of the most commonly used plastics today and has a wide variety of uses, such as a manufacturing material and as a packaging material.

To produce light olefins, the catalytic cracking of heavy hydrocarbon feedstocks, such as naphtha, is typically performed by contacting a naphtha containing feed with a catalyst composition that normally comprises one or more crystalline microporous molecular sieves to selectively convert the feed to an olefin-containing mixture. Although various naphtha catalytic cracking processes have been proposed in the past, many of the processes do not produce commercially important light olefins, for example propylene, with sufficient selectivity or yield. Likewise, cracking processes can produce undesirable amounts of methane and aromatics as unwanted byproducts. In contrast, a practical and economical naphtha catalytic cracking process should selectively produce increasing amounts of light olefins, for example propylene, while producing minimal amounts of methane and aromatics.

In FCC processes, a hydrocarbon feedstock is injected into the rising section of an FCC reactor, where the raw material is cracked into lighter and more valuable products, after contact with a heated catalyst that is circulated through the reactor. elevator from a catalyst regenerator. One of the main advances in FCC catalysts occurred in the early 60s, with the introduction of molecular sieves or zeolites. These materials were incorporated into the matrix of amorphous materials and / or amorphous materials / kaolin that were the FCC catalysts of that time. These new zeolitic catalysts, which contained a crystalline aluminosilicate zeolite in a matrix of amorphous material or amorphous material / kaolin of silica, alumina, silica-alumina, kaolin, clay or the like were at least 1,000-10,000 times more active for cracking hydrocarbons that the previous amorphous silica-alumina catalysts or that contained amorphous material / kaolin. This introduction of zeolitic cracking catalysts revolutionized the fluid catalytic cracking process. New processes were developed to manipulate these large activities, such as rising cracking, shorter contact times, new regeneration processes, new developments of improved zeolitic catalyst and the like.

The zeolites typically used in FCC are crystalline aluminosilicates having a uniform crystalline structure characterized by a large number of small regular cavities interconnected by a large number of even smaller channels. It was discovered that, thanks to this structure consisting of a network of cavities and channels of uniform size, the crystalline zeolites are able to accept, by absorption, molecules that have sizes below a certain well-defined value, while molecules were rejected. of larger sizes and, for this reason, they have been given the name of "molecular sieves". This characteristic structure also gives them catalytic properties, especially for certain types of hydrocarbon conversions.

In current commercial practice, most of the FCC cracking catalysts used throughout the world are manufactured from a large pore zeolite as a catalytically active component. Conventional large pore molecular sieves include zeolite X; REX; Y zeolite; And Ultrastable (USY); And with exchange of Rare Earths (KING); USY with exchange of Rare Earths (REUSY); And dealuminated (DeAl Y); And Ultrahydrophobic (UHPY); and / or dealuminated silicon enriched zeolites, for example LZ-210. ZSM-20, zeolite L and zeolites of natural origin such as faujasite, mordenite and the like have also been used.

In addition to the large pore zeolites, the ZSM family of zeolites is well known and its preparation and properties have been extensively described in the catalytic cracking of hydrocarbons. For example, one type of ZSM zeolite family is known as ZSM-5. The crystalline aluminosilicate zeolite known as ZSM-5 is disclosed in particular in U.S. Patent No. 3,702,886, the disclosure of which is incorporated herein by reference. The crystalline aluminosilicate ZSM-5 is characterized by a molar ratio of silica to alumina greater than 5 and, more precisely, in the anhydrous state, by the general formula: [0,9, + -, 0,2M.2 / nO: Al2O3: > 5SiO2] in which M has a valence n selected from the group consisting of a mixture of cations of alkali metal and organoammonium cations, particularly a mixture of sodium and tetraalkyl ammonium cations, which alkyl groups preferably contain from 2 to 5 carbon atoms. The term "anhydrous", as used in the above context, means that molecular water is not included in the formula. In general, the molar ratio of Si02 to Al203 for a ZSM-5 zeolite can vary widely. For example, zeolites ZSM-5 can be free of alumina, in which ZSM-5 is formed from an alkaline silica mixture containing only aluminum impurities. However, all zeolites characterized as ZSM-5 will have the characteristic X-ray diffraction pattern set forth in U.S. Patent No. 3,702,886, regardless of the aluminum content of the zeolite.

Zeolite beta is another zeolite that can be used in the catalytic cracking of hydrocarbons. Beta zeolite is typically a large pore zeolite rich in silicon having a three dimensional pore structure, and having both acidic catalytic properties and structural selectivity, due to its structural peculiarity, and also has a very high thermostability (the temperature of failure). of the crystalline network is greater than 1200 ° C), hydrothermal stability and abrasion resistant properties. Due to the unique structural characteristics thereof, zeolite beta has good thermal and hydrothermal stability, acid resistance, anti-coking properties and catalytic activity in a series of catalytic reactions. Therefore, it has developed rapidly for new catalytic processes in recent years.

The catalysts used in the FCC process have been customized to maximize the performance in the specific hydrocarbon conversion processes. For example, the catalyst compositions used in the hydrocarbon conversion processes have been prepared in multifunctional catalysts, for example, a bifunctional catalyst or a trifunctional catalyst. A bifunctional catalyst comprises two different catalysts, for example two zeolites having different compositions or types of structure that induce different reactions. The reaction products may be different or the two catalysts may be used together so that the reaction product of a catalyst is transported to and reacts on a catalyst site of the second catalyst. Also, since one of the benefits of using a zeolite catalyst is that the catalyst has a selective and non-selective form, the reactions on the surface of the zeolite are usually not desirable, the zeolite catalysts used in the hydrocarbon conversion processes have the ability to avoid, or at least reduce, the undesirable reactions that may take place on the surface of the catalyst of zeolite selectively screening the molecules in the feed stream based on their shape or size. In this way, undesirable molecules present in the feed stream are prevented from entering the pores of the catalyst and reacting. In addition, the yield of a zeolite catalyst can sometimes be maximized if the catalyst selectively screens the desired molecules based on their size or shape, to prevent the molecules from leaving the pores of the catalyst.

Hydrocarbon conversions using catalyst compositions containing two different zeolites have been used in the past. For example, to increase the octane number of the gasoline fraction, a catalyst composition containing a large pore molecular sieve, such as zeolite Y, as the primary cracking component and a medium pore zeolite, such as ZSM- 5, added to the zeolite Y cracking catalyst, is typically used in conventional processes for the catalytic cracking of heavy hydrocarbon feedstocks for gasoline and distillate fractions. U.S. Patent No. 3,758,403 discloses a catalyst using a ZSM-5 zeolite and a large pore zeolite, such as zeolite Y (with a ratio of 1: 10 to 3: 1) as active components. In addition to boosting the octane number of gasoline, this catalyst mixture provides a higher yield of C3 and C4 olefins.

From U.S. Patent No. 5,279,726 and EP 559,646 it is also known, for example, how to form compounds of two different aluminosilicates, a Y zeolite and a zeolite beta for use in the cracking of hydrocarbons. In U.S. Patent No. 5,279,726, a hydrocracking catalyst having high activity and selectivity for gasoline comprising a hydrogenation component on a catalyst support comprising both zeolite beta and a zeolite Y is disclosed. U.S. Patent No. 5,536,687 involves a hydrocracking process using a catalyst containing crystals of zeolite beta and zeolite Y that are bound by an amorphous binder material such as alumina.

In addition, documents CN 1103105A and EP-2-075-068 A1 describe the use of catalyst compositions comprising three different zeolites in the cracking of hydrocarbons. CN 1 103105A discloses a cracking catalyst capable of giving a higher yield of isobutene and isopentene than without the catalyst and can coproduce high octane gasoline. The components and contents of the catalyst described in CN 1103105A are the following: (1) 5-25% by weight of HZSM-5 modified with a silicon: aluminum ratio of 20-100; (2) 1-5% by weight of HZSM of high silicon content with a silicon: aluminum ratio of 250-450; (3) 5-20% by weight of USY zeolite; (4) 1-5% by weight of zeolite beta; (5) 30-60% by weight of natural clay; and (6) 15-30% by weight of inorganic oxide. EP-2-075-068 A1 discloses a catalyst composition with a zeolite mixture as follows: (1) 1-75% by weight of a phosphorus-modified beta-zeolite and a transition metal; (2) 25-99% by weight of a zeolite having an MFI structure, such as ZSM-5; and (3) 0-74% by weight of a large pore zeolite, such as a Y zeolite.

To increase the yields of light olefins during the hydrocarbon cracking process, a zeolite cracker catalyst with added phosphorus has been used. WO 98/41595 discloses that the addition of a phosphorus-containing medium pore zeolite, such as ZSM-5, to a molecular sieve cracking catalyst with conventional pore size, increases the yield of C3 to C5 olefins in the catalytic cracking of hydrocarbon raw materials without a significant loss in the aging characteristics of the medium pore additive. In this manner, the yield of C4 and C5 olefins in catalytic cracking can be enhanced by adding a phosphorus-containing medium pore zeolite, such as ZSM-5, to a conventional Y-zeolite cracking catalyst.

The incorporation of phosphorus into the medium pore zeolite is conventionally achieved by the methods described in U.S. Patent Nos. 4,356,338, 5,110,776 and 5,231,064. Treatment with phosphorus-containing compounds can be easily achieved by contacting the zeolite, either alone or in combination with a binder or matrix material, with a solution of an appropriate phosphorus compound, followed by drying and calcining to convert the phosphorus. in its oxide form.

Although the current FCC process in which various combinations of Y zeolite, zeolite beta and ZSM-5 are used is an effective process to convert a heavier feed to lighter products, often the process produces lower than desirable quantities of olefins. light as propylene. The growth in the propylene market is expected to drive the demand for propylene, and a propylene production process is desired through an FCC process that is more selective towards propylene than the catalyst compositions of the prior art.

Summary of the invention The aim of this invention is to develop a combination of petrochemical fluid catalytic cracking catalyst that results in a significant increase in the propylene yield compared to the current state of the petrochemical FCC catalyst systems of the art. This invention complements the known combinations of zeolite Y and ZSM-5, with an additional additive containing beta zeolite.

Detailed description of the invention The objective of this invention is to develop a petrochemical FCC catalyst system that results in a significant increase in the propylene yield compared to the current state of the petrochemical FCC catalyst systems of the art. Current petrochemical catalyst systems typically consist of a combination of a large pore catalyst, such as an FCC catalyst based on zeolite Y, and an additive zeolite such as ZSM-5. This invention proposes to complement the current catalyst combination with a beta zeolite containing additional additive.

To achieve the desired increase in propylene yield, the present invention provides a catalyst combination, comprising, based on the total weight of the catalyst combination, 5-50% by weight of Y zeolite, 5-40% by weight of ZSM-5 and 35-70% of Beta catalyst. In another embodiment, the catalyst composition comprises 25-30% by weight of zeolite Y, 15-20% by weight of ZSM-5 and 50-60% of catalyst Beta. The percentage by weight for each zeolite, as expressed immediately above and below, including the appended claims, refers to the active zeolite component and to any matrix, binder or components additives FCC catalysts are often combinations of a catalytically active large pore zeolite component and additives containing other zeolites. Large pore cracking catalysts have pore openings greater than about 7 Angstrom effective diameter. Conventional large pore molecular sieves include zeolite X (U.S. Patent No. 2,882,442); REX; Y zeolite (U.S. Patent No. 3,130,007); And Ultrastable (USY) (U.S. Patent No. 3,449,070); And with Rare Earth Exchange (KING) (U.S. Patent No. 4,415,438); USY with exchange of Rare Earths (REUSY); And De-aluminate (From Al Y) (U.S. Patent Nos. 3,442,792 and 4,331,694); And Ultrahydrophobic (UHPY) (U.S. Patent No. 4,401,556); and / or dealuminated silicon enriched zeolites, for example LZ-210 (U.S. Patent No. 4,678,765). The higher silica forms of the Y zeolite are generally preferred. The ZSM-20 (U.S. Patent No. 3,972,983) and the L zeolite (U.S. Patent Nos. 3,216,789 and 4,701,315); and also zeolites of natural origin such as faujasite, mordenite and the like (with all previous patents in parentheses incorporated herein by reference) can also be used. These materials can be subjected to conventional treatments such as impregnation or exchange of ions with rare earths to increase stability. In current commercial practice most catalysts contain these large pore molecular sieves.

Other large-pored crystalline molecular sieves include pillar-shaped silicates and / or clays; aluminophosphates, for example AIPO.sub.4-5, AIPO.sub.4-8, VPI-5; silicoaluminophosphates, for example SAPO-5, SAPO-37, SAPO-40, MCM-9; and other metal aluminophosphates. The mesoporous crystalline material for use as the molecular sieve includes MCM-41. These are described variously in the State Patents United N ° 4,310,440; 4,440,871; 4,554,143; 4,567,029; 4,666,875; 4,742,033; 4,880.61 1; 4,859,314; 4,791,083; 5,102,643; and 5,098,684, each incorporated herein by reference.

The preferred molecular sieve of those indicated above is a Y zeolite, more preferably a REY, USY or REUSY. In general, zeolite Y is incorporated into an amorphous binder in a manner well known in the art. Suitable binders include silica, silica-alumina, alumina, clay or other known inorganic binders.

In another embodiment of the invention, zeolite Y could be produced in high zeolite content microspheres by the in situ process described in U.S. Patent No. 4,493,902, the teachings of which are incorporated herein by cross-reference. The '902 patent discloses new fluid cracking catalysts comprising catalytically active, high zeolitic, wear resistant microspheres containing more than about 40%, preferably 50-70% by weight of faujasite Y, and methods for making such catalysts crystallizing more than about 40% sodium zeolite Y in porous microspheres composed of a mixture of metakaolin (calcined kaolin to undergo a strong endothermic reaction associated with dehydroxylation) and calcined kaolin under more severe conditions than those used to convert kaolin into metakaolin, that is, calcined kaolin to experience the exothermic reaction characteristic of kaolin, sometimes called the spinel form of calcined kaolin. The microspheres containing the two forms of calcined kaolin could also be immersed in the alkaline solution of sodium silicate, which is heated, preferably until the maximum obtainable amount of faujasite Y crystallizes in the microspheres.

In carrying out the invention described in the '902 patent, so that the microspheres Compounds of calcined kaolin undergo the exotherm and metakaolin are reacted with a caustic enriched sodium silicate solution in the presence of a crystallization initiator (seeds) to convert the silica and alumina into the microspheres in synthetic faujasite sodium (Y zeolite). The microspheres are separated from the sodium silicate mother liquor, the ions are exchanged with rare earths, ammonium ions or both to form rare earths or various known stabilized forms of the catalysts. The technology of the "902 patent provides means to achieve a desirable and unique combination of a high zeolite content associated with high activity, good selectivity and thermal stability, as well as wear resistance.

In another embodiment of the invention, zeolite Y could be produced as new zeolite microspheres, known as the Naphthamax® catalyst from BASF Catalysts, which is disclosed in U.S. Patent No. 6,656,347. These zeolite microspheres are macroporous, have sufficient levels of zeolite to be very active and are unique in morphology to achieve efficient conversion of hydrocarbons to cracked gasoline products with improved cracking glues in a FCC process with a contact time short. The new zeolite microspheres are produced by a new processing, which is a modification of the technology described in the '902 patent. It has been found that, if the new zeolite-rich alumina-free matrix of the catalyst is obtained from a source of ultra-fine water kaolin having a particle size such that 90% by weight of the water kaolin particles are smaller than 2 micrometers, and which is pulverized and calcined through the exotherm, a macroporous zeolite microsphere can be produced. More generally, the FCC catalyst matrix useful to achieve the macroporosity of the FCC catalyst is obtained from alumina sources, such as the kaolin calcined through the exotherm, which has a specified pore volume of water, which distinguish from calcined kaolin in the prior art used to form the catalyst matrix. The water pore volume is obtained from the Incipient Suspension Point (ISP) test that is described in the patent.

The morphology of the microsphere catalysts formed is unique with respect to the previously formed microsphere in situ catalysts. The use of an ultrafine pulverized water kaolin calcined through the exotherm produces in situ zeolite microspheres having a macroporous structure in which the macropores of the structure are coated or coated essentially with zeolite after crystallization. Macroporosity as defined herein means that the catalyst has a volume of macropores in the pore range of 600-20,000 Angstrom of at least 0.07 cm 3 / g of mercury intrusion, preferably at least 0.10 cm 3 / g of mercury intrusion. The new catalyst is optimal for an FCC process, including the short contact time of the process in which the hydrocarbon feed is contacted with a catalyst for times of about 3 seconds or less.

In the broadest sense, Naphthamax® as described in U.S. Patent No. 6,656,347, is not restricted to macroporous catalysts having a non-zeolite matrix derived solely from kaolin. In this manner, any source of alumina having the appropriate combinations of porosity and reactivity during the synthesis of zeolite and can generate the desired macroporosity and catalyst morphology can be used. The desired morphology comprises a matrix that is well dispersed through the catalyst, and the macroporous walls of the matrix are aligned with the zeolite and are substantially free of binding coatings. Consequently, not only is the large pore surface area of the catalyst greatly improved with respect to the previous catalysts, and the active matrix dispersed through of the microsphere, but the zeolite crystals are easily accessible to the hydrocarbon feed. Without wishing to be bound by any theory of operation, it appears that the previous catalysts in which the zeolite is incorporated into a matrix by physical mixing and stick with binder have a sufficient macroporosity, however the binder coats the active zeolite catalyst by blocking the this way the accessibility to it. The Naphthamax® microsphere catalysts have a morphology that allows rapid diffusion in the catalyst due to the macroporosity and enhanced dispersion of the matrix, and also provide greater accessibility to the zeolite insofar as the zeolite is coated freely on the walls of the porous. The term "freely" means that the zeolite phase is present on the surface of the matrix and is not obstructed by any binder phase. Simply by having macroporosity the results that have been obtained are not provided, since the conventional incorporated catalysts have a similar macroporosity. Therefore, the combination of porosity and macropore walls coated with zeolite gives the surprising selectivity results.

In another embodiment of the invention, zeolite Y is a Y zeolite with rare earth exchange crystallized in situ in a porous kaolin matrix. In another embodiment of the invention, the Y zeolite contains up to 12% of rare earth elements with ion exchange on the zeolite Y.

For the present invention, ZSM-5 is combined with zeolite Y. Based on the unique pore structure of ZSM-5, this zeolite can be applied extensively as a catalytic material to various processes. It has been shown that zeolite ZSM-5 is a particularly useful catalyst in reactions involving aromatic compounds, with emphasis on those having a single carbocycle. In this way, ZSM-5 presents unique selectivity in the conversion of olefins, naphienes, alcohols, ethers and allies in aromatic compounds and in reactions such as isomerization, alkylation, dealkylation and transalkylation of aromatics. This favorable influence on the aromatic conversion reactions is also found in the ZSM-5 forms in which another metal appears in isomorphic substitution for aluminum, as described in U.S. Patent No. 4,163,028. ZSM-5 has also been extensively applied in catalytic cracking and catalytic dewaxing. When ZSM-5 is used in petroleum catalytic cracking, it is possible to enhance the octane of gasoline. Accordingly, ZSM-5 has been used as an additive for other cracking catalysts, for example Y zeolite, to improve gasoline octane and LPG yields.

In another embodiment of the invention, the ZSM-5 zeolite additive is prepared as a separate microsphere and contains stabilized ZSM-5 zeolite, alumina and kaolin bound together with phosphoric acid.

ZSM-5 can be modified using phosphorus-containing compounds. Any phosphorus-containing compound having a covalent or ionic constituent capable of reacting with the hydrogen ion, such as for example phosphoric acid, phosphines and phosphites, can be employed. Suitable phosphorus-containing compounds include derivatives of groups represented by PX3, RPX2, R2 PX, R3 P, R3 P = 0, RP02, RP (0) (OX) 2, R2 P (0) OX, RP (OX) 2 , ROP (OX) 2 and (RO) 2 POP (OR) 2 where R is an alkyl or phenyl radical and X is hydrogen, R or halide. These compounds include primary phosphines, RPH2, secondary R2PH and tertiary R3P such as butyl phosphine; the tertiary phosphine oxides, R3PO such as tributylphosphine oxide; the primary phosphonic acids RP (0) (OX) 2 and secondary R2P (0) OX such as benzene phosphonic acid; esters of phosphonic acids such as diethyl phosphonate, (RO) 2P (0) H, dialkyl alkyl phosphonates, (RO) 2P (0) R and alkyl dialkylphosphinates (RO) P (0) R2; Phosphine acids, R2POX, such as diethylphosphinous acid, primary phosphites (RO) P (OX) 2, secondary (RO) 2POX and tertiary (RO) 3P; and esters thereof such as monopropyl ether, esters of alkyl dialkylphosphinites, (RO) PR2 and dialkyl alkylphosphonite (RO) 2PR. Examples of phosphite esters include trimethylphosphite, triethylphosphite, diisopropylphosphite, butylphosphite and pyrophosphates, such as tetraethylpyrofosphite. The alkyl groups in the mentioned compounds contain from 1 to 4 carbon atoms.

Other suitable phosphorus-containing compounds include phosphorus halides such as phosphorus trichloride, bromide and iodide, alkyl phosphorodichloridites (RO) PCI.sub.2, dialkyl phosphorochloridites (RO) 2PX, dialkylphosphinochlorites, R2PCI, alkyl alkylphosphonchloridates, (RO) ( R) P (0) CI and dialkyl phosphinohydrochlorides, R2P (0) CI.

Preferred phosphorus-containing compounds include: phosphoric acid, ammonium dihydrogen phosphate, diammonium hydrogen phosphate or ammonium polyphosphate, trimethyl phosphite and phosphorus trichloride.

It is believed that the constituent of the phosphorus-containing compound capable of reacting with the hydrogen ion reacts with the hydrogen of the original zeolite. This would suggest that the phosphorus could chemically bind to the crystalline structure of the zeolite, since zeolites containing phosphorus can be used for extended periods of time at high temperatures without loss of phosphorus. Additionally, it is unlikely that phosphorus is present as a constituent of the crystal structure, that is, it has not been replaced by silicon or aluminum atoms, since the dimensions of the unit cell of the zeolite do not change by the incorporation of the phosphorus atoms.

The incorporation of the phosphor with the zeolite provides a composition that has unique properties as a catalytic agent. Zeolites have strong acid sites. On the other hand, phosphorus-containing zeolite does not possess these strong acid sites. The phosphorus-containing zeolite has a higher number of acid sites than the zeolite precursor, but these sites appear to have a lower acid potency than those found in the precursor zeolite. It is believed that the apparent substitution of strong acid sites for a greater number of relatively weak acid sites may be responsible for the unique catalytic properties of the phosphorus-containing zeolite.

The reaction of the zeolite with the phosphorus-containing compound is carried out by contact. When the phosphorus-containing compound is a liquid, said compounds may be in solution in a solvent at the time the contact with the zeolite is made. Any relatively inert solvent can be used with respect to the phosphorus-containing compound and the zeolite. Suitable solvents include aliphatic, aromatic or alcoholic liquids. When the phosphorus-containing compound is trimethylphosphite or liquid phosphorus trichloride, a hydrocarbon solvent such as n-octane may be employed. The phosphorus-containing compound can be used without a solvent, that is, it can be used as a pure liquid. When the phosphorus-containing compound is in the gas phase, such as when phosphorus trichloride gas is used, the phosphorus-containing compound can be used by itself or can be used mixed with a gaseous diluent relatively inert to the phosphorus-containing compound and the zeolite, such as air or nitrogen.

Preferably, before reacting the zeolite with the phosphorus-containing compound, the zeolite is dried. The drying can be carried out in the presence of air. High temperatures can be used. However, the temperature should not be so high, as mentioned above, so as to destroy the crystal structure of the zeolite.

The heating of the phosphorus-containing catalyst after the preparation and before use is also preferred. The heating can be carried out in the presence of oxygen, for example air. The heating can be at a temperature of approximately 150 ° C. However, higher temperatures are preferred, that is, up to about 500 ° C. The heating can be carried out for 1-24 hours. It has been found that heating increases the catalytic efficiency of the phosphorus-containing zeolite, probably due to an increase in the number of acid sites rather than an increase in the strength of existing acid sites. Increasing the heating temperature increases the efficiency of the catalyst. However, although heating temperatures above about 500 ° C may be employed, they are not necessary. At temperatures of about 1000 ° C, the crystalline structure of the zeolite is destroyed.

The amount of phosphorus incorporated with the crystal structure of the phosphorus-containing zeolite should be at least 0.1% by weight. With this amount of phosphorus, a sufficient proportion of strong acid sites of the zeolite is replaced with a greater number of weaker acid sites. To achieve this, it is preferred that the amount of phosphorus in the phosphorus-containing zeolite be at least about 0.5% by weight. The amount of phosphorus can be as high as 10% by weight, although with these higher amounts a decrease in catalytic activity can occur.

In addition, the large-pore molecular sieve catalytic component described above may also include phosphorus or a phosphorus compound for any of the functions generally attributed thereto.

As discussed above, ZSM-5 selectively cracks aliphatic molecules in the gasoline range to form additional light olefins at the expense of gasoline yield. Using ZSM-5 containing phosphorus as FCC additives instead can reduce the loss of gasoline yield and still effectively enhance the yields of light olefin. The yields of 2-methyl-butenes and n-butenes increase also when ZSM-5 containing phosphorus is used as the additive, due to its more moderate acid potency. On the other hand, untreated ZSM-5 will additionally crack these C5 and C4 olefins due to their high acid potency. Therefore, when the phosphorus-containing ZSM-5 zeolites are used as additives for cracking catalysts, the yields of 2-methyl-butenes, n-butenes and gasoline are improved using the corresponding untreated ZSM-5 as an additive.

In another embodiment of the invention, zeolite ZSM-5 is combined with zeolite Y, in which the ZSM-5 zeolite additive is prepared according to U.S. Patent No. 7,375,048. According to the '48 patent, a slurry of high solids kaolin is mixed with a suspension containing ZSM-5, an alumina of high surface area (pseudobohemite type) and a low surface area alumina or non-reactive inorganic material of similar high density. The mixed suspension is pumped to a static mixer adjacent to the atomizer of the spray dryer. Phosphoric acid is then injected into the highly dispersed solids mixed with the kaolin suspension and the suspension injected with acid is sprayed into droplets in a spray dryer. The process provides microspheres that have good interparticle bonding and excellent physical and chemical properties. In addition, the microspheres may contain at least 30% by weight of ZSM-5 and, due to the addition of the non-reactive alumina or other high-density non-reactive inorganic material, have a high wear resistance.

For the present invention, beta zeolite is added to the combination of zeolite Y and zeolite ZSM-5. Beta zeolite is a crystalline zeolite whose composition and X-ray powder diffraction analysis are disclosed in U.S. Patent No. 28,341, incorporated herein by reference in its entirety. This zeolite is a large pore zeolite that has a pore size above 7.0 Angstrom and an index of Restriction below 2. Zeolite beta is prepared, in general, as an aluminosilicate zeolite having a molar ratio of silica to alumina (Si02 / Al203) of at least 10. It can also be prepared at molar ratios of silica to alumina larger, for example 500: 1 or greater, and although such materials may have little or no zeolitic properties, it should be understood that, in the present invention, the term "zeolite beta" is intended to encompass such materials.

The beta zeolite is usually synthesized from a reaction mixture containing a template agent. The use of template agents to synthesize zeolite beta is well known in the art. For example, U.S. Patent No. 3,308,069 and Re N 28,341 describe the use of tetraethylammonium hydroxide and U.S. Patent No. 5,139,759, which is incorporated herein by reference in its entirety, describes the use of tetraethylammonium ion derived from the corresponding tetraethylammonium halide. Another conventional method for preparing beta zeolite is described in the book entitled Verified Synthesis of Zeolitic Materials, by H. Robson (editor) and KP Lillerud (Patterns of XRD), second revised edition, ISBN 0-444-50703-5, Elsevier, 2001. It is believed that the choice of a particular template agent is not critical to the success of the process disclosed in this document. In one embodiment, the beta zeolite is calcined in air at a temperature of 500 to 700 ° C for a sufficient time to remove to remove the template agent from the beta zeolite. The calcination to remove the template agent can be carried out before or after the beta zeolite is combined with the support and / or the hydrogenation component. Although it is believed that the stencil agent could be removed at calcination temperatures above 700 ° C. Very high calcination temperatures could significantly decrease the SF6 adsorption capacity of zeolite beta. For this reason, it is believed that calcination temperatures above 750 ° C should be avoided to remove the stencil agent when preparing beta zeolite for use in the process disclosed in this document. It is critical for the process disclosed herein that the SF6 adsorption capacity of the zeolite beta be at least 28% by weight.

However, synthesis of zeolite beta without template has been demonstrated in US Published Application No. US1010 / 0322847, by BASF. In another embodiment of the invention, the additive for zeolite beta for the present invention is prepared in a manner similar to the additive ZSM-5 according to U.S. Patent No. 7,375,048.

In still another embodiment of the invention, the form of the zeolite Beta is H-Beta, with a silica / alumina ratio greater than 10, further exemplified by silica / alumina ratios greater than 35. The silica / alumina ratio of the H-Beta zeolite can also be greater than 100.

The stabilization of the phosphorus beta zeolite in the present invention can be achieved by direct reaction of the Beta zeolite with phosphoric acid or by incorporation of the phosphoric acid into the additive by direct injection during the spray drying process. The ammonium hydrogen phosphates, or polyphosphates, can also be used, as described above for the ZSM-5 additive.

In another embodiment of the invention, the phosphorus level in the beta zeolite is between 1 and 7% of P205.

In another embodiment of the invention, the phosphorus level in the beta zeolite is between 3 and 5% of P205. The addition of phosphoric acid by in-line injection during spray drying of the beta additive required a total phosphorus level of between 10 and 15% of 205 205, with a more preferred level of 12-13% of P205.

In another embodiment of the invention, the zeolite Y is Naphthamax® (zeolite Y with rare earth exchange crystallized in situ in a porous kaolin matrix) and combined with the ZSM-5 zeolite-containing additive described above. It adds a additive in the form of different catalyst particles, containing Beta zeolite, described above, to the catalyst combination.

Example 1 Combinations of the Beta additive with Naphthamax® exchanged with rare earths in low amount and ZSM-5 additive after steam deactivation (15-24 hours at 1500 ° F and 100% steam) have been evaluated in the ACE ™ using a paraffin raw material supplied by Reliance Industries. Beta zeolite has a high propensity to create olefins due to its low intrinsic hydride transfer capacity. This can be observed in the high levels of isobutylene to isobutane in the cracking reactions. Therefore, the combination ratios for a maximum propylene yield are based on more Beta additive than Naphthamax® and more Naphthamax® than ZSM-5 additive. Such formulation would be 50-60% Beta additive, 25-30% REO Naphthamax® 1% and 15-20% ZSM-5 additive. Such formulation gives propylene yields of 1.5-2.5%, higher than with the current state of the petrochemical FCC catalyst of the art.

Single-point catalyst / oil cracks were made in the ACE of eight combinations: four using 50% Beta catalyst and four using 60% Beta catalyst. The amounts of ZSM-5 and Naphthamax® were then varied to balance the combination. Table 1 gives the combination ratios and the conversions and yields of propylene at a C / O of 10.26.

Table 1 It can be seen from Table 1 that the combinations C, D and F have the highest propylene yields and an acceptable activity.

Example 2 A catalyst composition composed of a combination of 60% Beta additive, 25% REO Naphthamax 1% and 15% additive ZSM-5 was prepared. The propylene yield of this catalyst composition is compared to a prior art petrochemical FCC catalyst containing 23.5% ZSM-5 additive and 76.5% REO Naphthamax 1%. The ACE test using a Reliance feed gave an increase in propylene yield of more than 2%.

Claims

1. A hydrocarbon conversion catalyst comprising, based on the total weight of the catalyst, a combination of: (a) from 5 to 50% by weight of a Y zeolite; (b) from 5 to 40% by weight of a ZSM-5 zeolite; Y (c) from 35 to 70% by weight of a Beta zeolite.

2. The catalyst of claim 1, wherein the zeolite Y is a macroporous zeolite containing zeolite Y crystallized as a layer on the surface of a matrix containing porous alumina, said laminated zeolite matrix being arranged in a configuration to provide macropores in that the zeolite layer is provided on the walls of the macropores.

3. The catalyst of claim 1, wherein the Y zeolite contains up to 12% of ions of rare earth elements exchanged on the Y zeolite.

4. The catalyst of claim 1 wherein each of the ZSM-5, the zeolite Beta and the zeolite Y is a distinct microsphere.

5. The catalyst of claim 1 wherein the ZSM-5 additive contains ZSM-5 zeolite stabilized with phosphorus, alumina and kaolin bound together with a phosphorus-containing compound.

6. The catalyst of claim 1 wherein the zeolite Beta is an H-Beta with a silica / alumina ratio greater than 10.

7. The catalyst of claim 6 wherein the silica / alumina ratio of the zeolite beta is greater than 100.

8. The catalyst of claim 1 wherein the Beta zeolite is modified with a phosphorus-containing compound.

9. The catalyst of claim 8 wherein the zeolite Beta has a phosphorus level between 1-7% P2O5.

0. The catalyst of claim 9 wherein the phosphorus level is between 3-5% of P205.

11. The catalyst of claim 1 wherein the catalyst comprises 25-30% by weight of zeolite Y, 15-20% by weight of ZSM-5 and 50-60% of zeolite Beta.

12. A hydrocarbon conversion catalyst comprising a combination of: (a) a Y zeolite, wherein the Y zeolite is a macroporous zeolite comprising Y zeolite crystallized as a layer on the surface of a porous alumina containing matrix, said laminated zeolite matrix being arranged in a configuration to provide macropores, wherein the zeolite layer is provided on the walls of the macropores. (b) a ZSM-5 zeolite; Y (c) a Beta zeolite.

13. The catalyst of claim 12 wherein the catalyst comprises 5-50% by weight of zeolite Y, 5-40% by weight of ZSM-5 and 35-70% of zeolite Beta.

14. The catalyst of claim 12 wherein the catalyst comprises 25-30% by weight of zeolite Y, 15-20% by weight of ZSM-5 and 50-60% of zeolite Beta.

15. The catalyst of claim 12 wherein the ZSM-5 zeolite is a ZSM-5 zeolite stabilized with phosphorus, alumina and kaolin bound together with a phosphorus-containing compound.